MATERIAL BALANCE

The above figure shows the simplified model of actual flow diagram. Since steam isadded to the reaction system in order to supply the heat of reaction to the endothermicdehydrogenation and the assumption we made that, there the solubility of the organicphase in the aqueous phase is negligible and water been separated completely in thedecanter so water will act as a inert in the material balance and can be neglected.SPECIFICATIONS:Selectivity to styrene conversion= 95%Selectivity to toluene conversion=3%Selectivity to benzene conversion=2%Let us assume the wt fraction of ethyl benzene in the recycle stream= 50%For the benzene-toluene column:Distillate composition= 90% (benzene+toluene)Residue composition=1% (benzene+toluene)For the EB recycle column:Distillate composition= 50% of EBResidue composition= 5% of EBFor the final styrene purification column:Distillate composition= 99% of styreneResidue composition = 2.3% of styreneBASIS: 100 kg of pure EB feed per hour.Let, “R” is the recycle stream ratio to that of the pure feed. i.e. For 100 kg of pure EBfeed recycle stream is 100*R kg.Therefore, total ethyl benzene feed to the reactor = (100 +100*R*0.5) kgWt composition in the stream leaving the reactor;Unreacted EB (W 0 ) = 0.35*(100 +100*R*0.5) kgStyrene (W 1 ) = [100*R*0.5 + 0.65*(100 +100*R*0.5)*0.95*104/106] kg